CN216236502U - Landfill leachate treatment system - Google Patents
Landfill leachate treatment system Download PDFInfo
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- CN216236502U CN216236502U CN202122257482.7U CN202122257482U CN216236502U CN 216236502 U CN216236502 U CN 216236502U CN 202122257482 U CN202122257482 U CN 202122257482U CN 216236502 U CN216236502 U CN 216236502U
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- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 106
- 239000012528 membrane Substances 0.000 claims abstract description 71
- 238000001704 evaporation Methods 0.000 claims abstract description 60
- 230000008020 evaporation Effects 0.000 claims abstract description 59
- 238000001471 micro-filtration Methods 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000004062 sedimentation Methods 0.000 claims abstract description 25
- 230000009615 deamination Effects 0.000 claims abstract description 24
- 238000006481 deamination reaction Methods 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 24
- 238000009279 wet oxidation reaction Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 230000015271 coagulation Effects 0.000 claims abstract description 20
- 238000005345 coagulation Methods 0.000 claims abstract description 20
- 239000002253 acid Substances 0.000 claims abstract description 4
- 239000000084 colloidal system Substances 0.000 claims abstract description 4
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- 239000002245 particle Substances 0.000 claims description 8
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- 238000010521 absorption reaction Methods 0.000 claims description 6
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- 238000007254 oxidation reaction Methods 0.000 claims description 5
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- 239000006228 supernatant Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
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- 238000006386 neutralization reaction Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 239000001117 sulphuric acid Substances 0.000 claims description 3
- 235000011149 sulphuric acid Nutrition 0.000 claims description 3
- 238000001514 detection method Methods 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 239000007800 oxidant agent Substances 0.000 claims description 2
- 239000012466 permeate Substances 0.000 claims description 2
- 239000000243 solution Substances 0.000 claims 6
- 239000012527 feed solution Substances 0.000 claims 1
- 238000011085 pressure filtration Methods 0.000 claims 1
- 239000012452 mother liquor Substances 0.000 abstract description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 4
- 150000003863 ammonium salts Chemical class 0.000 abstract description 4
- 229910052791 calcium Inorganic materials 0.000 abstract description 4
- 239000011575 calcium Substances 0.000 abstract description 4
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- 239000011777 magnesium Substances 0.000 abstract description 4
- 229910052710 silicon Inorganic materials 0.000 abstract description 4
- 239000010703 silicon Substances 0.000 abstract description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 abstract description 3
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 abstract 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract 1
- 239000006227 byproduct Substances 0.000 abstract 1
- 239000012153 distilled water Substances 0.000 abstract 1
- 229910052731 fluorine Inorganic materials 0.000 abstract 1
- 239000011737 fluorine Substances 0.000 abstract 1
- 229920006395 saturated elastomer Polymers 0.000 abstract 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
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- 231100000719 pollutant Toxicity 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
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- 239000004902 Softening Agent Substances 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
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- 235000011116 calcium hydroxide Nutrition 0.000 description 3
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- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- 235000019270 ammonium chloride Nutrition 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- -1 suspended matters Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000003403 water pollutant Substances 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
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- 230000002035 prolonged effect Effects 0.000 description 1
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Abstract
The utility model relates to a landfill leachate treatment system which comprises a pretreatment unit, a coagulation reaction tank, a sedimentation tank, a raw water concentration tank, a microfiltration membrane unit, an evaporation unit, a micro-interface wet oxidation unit and a deamination membrane unit. The utility model comprehensively pretreats raw leachate water through a pretreatment unit, a coagulation reaction tank and a microfiltration membrane unit to remove suspended matters, colloids, calcium, magnesium, silicon, fluorine and alkalinity contained in the raw water. The micro-interface wet oxidation unit is used as an evaporation process bypass flow treatment unit, so that the COD of the mother liquor is reduced, the COD enrichment degree of the evaporation concentrated solution is controlled, the reliable operation of the evaporation unit is ensured, and the discharge amount of the concentrated solution is reduced. The evaporation unit adopts an evaporation device to evaporate raw water of the percolate, steam is condensed to be distilled water and is discharged, evaporated condensate water passes through the deamination membrane unit and is circularly absorbed by dilute acid to reduce ammonia nitrogen in the condensate water, and saturated circulating liquid is independently evaporated and crystallized to obtain a byproduct ammonium salt.
Description
Technical Field
The utility model belongs to the field of landfill leachate treatment, and particularly relates to a landfill leachate treatment system.
Background
With the rapid development of economy in China, the urban construction scale changes day-over and land-covering and the living standard of people is greatly improved, and meanwhile, the yield of household garbage is increased more and more. In 2017, the production amount of domestic garbage in China is up to 2.1 hundred million tons, the quantity of the garbage is increased by 8-13% per year, and the garbage yield is increased to 5.2 hundred million tons in 2020. In the process of landfill, various organic matters in the domestic garbage can generate various biochemical reactions under the action of microorganisms, and are gradually degraded to generate inorganic matters, salts, heavy metals and other pollutants, and the pollutants are greatly enriched in the leachate to form the landfill leachate of high-concentration pollutants. The landfill leachate has the characteristics of complex components, high pollutant concentration, high salt content, biological inhibition and the like, so that the treatment process is complex, and if the landfill leachate is not treated well, the human health and the ecological environment are seriously threatened.
Aiming at the leachate of the refuse landfill, the 'pretreatment + biochemical treatment + membrane component advanced treatment' is taken as a recommended main treatment process, and the process is adopted in a plurality of refuse landfills in China. However, the large volumes of concentrate produced by this process are back-filled for extended periods of time, resulting in a continuous increase in TDS and a continuous decrease in biodegradability of the leachate inventory. In recent years, a new process of 'MVC evaporation + ion exchange' is introduced into some landfill sites to replace the traditional process for treating landfill leachate, the quality of tail water discharged after the landfill leachate is treated by the process can reach the requirement of the water pollutant discharge concentration limit value specified in the second specification in the pollution control Standard of domestic landfill (GB16889-2008), and the operation cost is lower than that of the traditional main process, but in view of the great difficulty in treating the landfill leachate, certain problems in the mother liquor treatment in the operation of the evaporation process need to be further improved and broken through urgently. In the running process of the MVC evaporation and ion exchange process, along with the continuous concentration of the evaporation mother liquor, the COD (chemical oxygen demand) of the mother liquor is continuously enriched, and the discharge amount is large, so that on one hand, the boiling point of the feed liquor can be greatly increased, the crystallization is influenced, and the quality of the finished salt is reduced; on the other hand, the main COD content in the evaporation mother liquor is macromolecular organic matter, and the evaporation mother liquor is thick after concentration, so that a percolate feeding pipeline, a heat exchanger and an evaporation main body are easily polluted and blocked, the treatment efficiency is reduced, and the operation cost is increased. The ion exchange resin needs to be regenerated in the application process, the technical management requirement of the regeneration process is high, the resin is easily regenerated and is acidic, the pH value of the effluent water is not up to the standard, secondary pollutants such as waste water containing pollutants such as hydrochloric acid and ammonium chloride can be formed, the water quantity is large, and the treatment capacity of process equipment is indirectly reduced. Therefore, aiming at the problems and the defects of the existing treatment technology, the landfill leachate treatment process of the landfill site, which is provided by the application patent, is efficient, high in automation degree and strong in operability, is developed, and full-quantitative treatment of the landfill leachate is realized.
Disclosure of Invention
In order to solve the above problems, the present invention provides a leachate treatment system for a landfill. The landfill leachate treatment system combining evaporation, micro-interface wet oxidation and deamination membrane has the characteristics of strong operability, simple process, high automation degree, no secondary pollution, low equipment operation cost, convenient system management and the like.
The utility model discloses a landfill leachate treatment system, which comprises a pretreatment unit, a coagulation reaction tank, a sedimentation tank, a raw water concentration tank, a micro-filtration membrane unit, an evaporation unit, a micro-interface wet oxidation unit and a deamination membrane unit, wherein the pretreatment unit is used for treating a landfill leachate;
the pretreatment unit, the coagulation reaction tank, the sedimentation tank, the raw water concentration tank and the microfiltration membrane unit are sequentially connected;
the pretreatment unit adopts a full-automatic back-flushing filter and is used for removing a large amount of particles, suspended matters, colloids and the like contained in the percolate; a water outlet of a filter of the pretreatment unit is connected with a coagulation reaction tank;
the coagulation reaction tank comprises two reaction water tanks with communicated bottoms, stirring devices are arranged in the two reaction water tanks of the coagulation reaction tank, and calcium, magnesium and silicon ions in leachate are removed by adding chemical softening agents of hydrated lime, sodium carbonate and coagulant of ferric trichloride into the coagulation reaction tank; reaction tank overflow ports are uniformly formed in the upper parts of the two reaction tanks, and the coagulation reaction tank is communicated with the sedimentation tank through the reaction tank overflow ports;
the sedimentation tank is used for settling coagulated particles, and supernatant is obtained after the coagulated particles are settled; the upper part of the sedimentation tank is provided with a sedimentation tank overflow port, and supernatant flows into the raw water concentration tank through the sedimentation tank overflow port;
the water outlet of the raw water concentration tank is connected with the water inlet of the microfiltration membrane device through a pipeline by a lift pump, water circulation is carried out between the raw water concentration tank and the microfiltration membrane unit, and meanwhile, clear water filtered by the microfiltration membrane unit enters the evaporation unit;
the concentrated solution discharge port of the evaporation unit is connected with the micro-interface wet oxidation unit through a high-pressure pump, the micro-interface wet oxidation unit is used for oxidizing the concentrated solution and then returning to the evaporation unit, and the condensed water outlet end of the evaporation unit is connected with the deamination membrane unit.
Further, the microfiltration membrane unit comprises a microfiltration membrane device, a concentrated water tank and an intermediate water tank, wherein two concentrated water pipelines are arranged on the concentrated water side of the microfiltration membrane device, one concentrated water pipeline is connected with the raw water concentrated tank, the other concentrated water pipeline is connected with the concentrated water tank, concentrated water circulation is continuously performed between the raw water concentrated tank and the microfiltration membrane device, part of concentrated water collected by the microfiltration membrane device enters the concentrated water tank, membrane permeation water of the microfiltration membrane device reaches the clean water side of the microfiltration membrane device and then enters the intermediate water tank, the water outlet of the intermediate water tank is connected with the water inlet of the evaporation unit, and the intermediate water tank of the microfiltration membrane unit is provided with a pH detection device and an acid adding port for controlling the pH value of feed liquid entering the evaporation unit. The middle water tank is a microfiltration membrane produced water collecting tank. The microfiltration membrane device adopts a tubular microfiltration membrane.
Furthermore, the micro-interface wet oxidation unit comprises a preheater, a micro-interface wet oxidation reactor, a heat exchanger and a gas-liquid separator, concentrated solution discharged from a concentrated solution discharge port of the evaporation unit passes through the preheater and then reaches the micro-interface wet oxidation reactor, the micro-interface wet oxidation reactor uses high-pressure air or oxygen as an oxidant to carry out oxidation treatment on the concentrated solution, the concentrated solution after the oxidation treatment enters the gas-liquid separator, and a liquid outlet end of the gas-liquid separator is connected with the evaporation unit after part of heat is recovered by the heat exchanger; the tail gas generated by the micro-interface wet oxidation unit is mainly carbon dioxide and is directly discharged.
Further, the deamination membrane unit comprises a pH adjusting tank, a deamination membrane device and a buffer tank; the side of intaking of pH equalizing basin is connected to evaporation unit comdenstion water outlet end, the comdenstion water after the pH value is adjusted passes through pipeline access deamination membrane device, deamination membrane device shell process product water drains into the buffer pool, carry out acid-base neutralization in the buffer pool, direct discharge to reach standard after the pH callback, the tube side adopts sulphuric acid as the absorption liquid, the ammonia that sees through the film element in the feed liquid in the absorption shell side, ammonium sulfate purity can reach more than 98% after evaporating crystallization alone, can carry out recovery processing as the ammonium salt.
Further, the evaporation unit comprises an evaporation device and a tail gas treatment device, a non-condensable gas outlet of the MVR evaporation device is connected with the tail gas treatment device, non-condensable gas generated in the evaporation process is subjected to acid-base treatment in the tail gas treatment device and then is discharged up to the standard, and the evaporation device adopts an MVR evaporator.
Furthermore, pipelines are arranged at the bottom of the sedimentation tank, the bottom of the raw water concentration tank and the bottom of the concentrated water tank of the micro-filtration membrane unit, are connected to a sludge filter pressing device and are used for discharging sludge, and after the sludge filter pressing device filters the sludge, the liquid is returned to the sedimentation tank;
the utility model has the following beneficial effects:
(1) by utilizing the pretreatment and microfiltration membrane unit, suspended matters, colloid, calcium, magnesium, silicon and the like in water can be effectively removed, the system is simple to operate, the effluent meets the water inlet requirement of the evaporation unit, and the stability of the subsequent process is ensured.
(2) The micro-interface wet oxidation technology is used as a by-pass flow treatment system in the evaporation process, and the high-efficiency oxidation efficiency of the system is utilized, so that the COD (chemical oxygen demand) of the mother liquor can be effectively reduced, the discharge amount of the mother liquor is reduced, the enrichment of the COD in the mother liquor is avoided, and the service life and the cleaning period of evaporation equipment are prolonged. Meanwhile, the micro-interface wet oxidation technology can be adjusted by a system, a combination mode different from that of an evaporation technology is realized, and the flexibility and operability of the system are improved.
(3) The water quality of the effluent of the deamination membrane unit is stable, the deamination membrane unit is different from the traditional technology that the ion exchange resin deamination is adopted for condensate water, hydrochloric acid and ammonium chloride wastewater generated by the regeneration of the ion resin are avoided, the purity of ammonium salt produced at the concentrated water side is high, and the resource reutilization can be realized through recovery treatment.
(4) The whole treatment system is simple to operate, high in automation degree, flexible and changeable in system combination, stable in effluent quality, capable of solving the problems ubiquitous in the traditional evaporation technology and capable of realizing full-quantitative treatment of the landfill leachate.
By the leachate treatment system for the refuse landfill, the effluent quality meets the water pollutant emission concentration limit value requirement specified in table two in the pollution control Standard of domestic refuse landfill (GB 16889-2008).
Drawings
FIG. 1 is a schematic view of a landfill leachate treatment system disclosed in the present invention.
Detailed Description
The following further describes the specific implementation mode of the utility model with reference to the attached drawings, and comprises the following implementation steps:
as shown in fig. 1, a landfill leachate treatment system comprises a pretreatment unit, a coagulation reaction tank, a sedimentation tank, a raw water concentration tank, a microfiltration membrane unit, an evaporation unit, a micro-interface wet oxidation unit, and a deamination membrane unit.
The pretreatment unit adopts a full-automatic back-flushing filter, a filtering water outlet is directly connected to a coagulation reaction tank through a pipeline, and a large amount of particles, suspended matters and the like contained in the leachate are removed. The coagulation reaction tank consists of two reaction water tanks with communicated bottoms, chemical softening agents, namely hydrated lime, sodium carbonate and coagulant, namely ferric chloride are added into the percolate through chemical softening agents, the slaked lime, the sodium carbonate and the coagulant are added into the percolate through chemical softening agents, calcium, magnesium and silicon are removed through continuous uniform stirring in the reaction process, an overflow port is formed in the upper portion of the reaction tank, and the effluent is directly communicated with the sedimentation tank through the overflow port. The water inlet of the sedimentation tank is an overflow port of the coagulation reaction tank, and after the coagulation particles are settled, the supernatant flows into the raw water concentration tank through the overflow port. The effluent of the raw water concentration tank is connected with the water inlet of the microfiltration membrane device through a pipeline by a lift pump. And discharging sludge from the bottom of the sedimentation tank and the raw water concentration tank, feeding the sludge into a sludge filter pressing device, and returning the liquid to the sedimentation tank.
The microfiltration membrane unit comprises a microfiltration membrane device, a concentrated water tank and an intermediate water tank. The microfiltration membrane device adopts a tubular microfiltration membrane, the clear water side of the microfiltration membrane device is connected with an intermediate water tank, the intermediate water tank is used as a microfiltration membrane produced water collecting tank, and the pH value is adjusted back by adding acid in the intermediate water tank; the concentrated water pipeline at the concentrated water side is divided into two paths, wherein one path is connected with the raw water concentration tank, and the other path is connected with the concentrated water tank; and (4) after the concentrated water at the concentrated water side of the microfiltration membrane flows back to the raw water concentration tank for a period of time, extracting part of concentrated water and entering the concentrated water tank. The outlet pipeline of the concentrated water tank is connected with the sedimentation tank and a sludge discharge pipeline at the bottom of the raw water concentrated tank.
The evaporation unit comprises an evaporation device and a tail gas treatment device, the evaporation device adopts an MVR evaporator, a non-condensable gas outlet of the evaporation device is connected with the tail gas treatment device, and the tail gas is subjected to acid-base treatment and then is discharged after reaching the standard. The water inlet of the evaporation device is connected with the water outlet of the middle water pool, and the concentrated solution discharge port of the evaporation device is connected into the micro-interface wet oxidation unit through a high-pressure pump; the condensed water outlet end of the evaporation device is connected with a deamination membrane unit.
The micro-interface wet oxidation unit comprises a micro-interface wet oxidation reactor, a preheater, a heat exchanger and a gas-liquid separator, wherein an evaporation concentrated solution discharge port is connected with the preheater through a pipeline and used for preheating the evaporation concentrated solution; the evaporation concentrated solution after oxidation treatment enters a gas-liquid separator, and a liquid outlet end is connected with an evaporation unit after part of heat is recovered by a heat exchanger; the tail gas generated by the system is mainly carbon dioxide and is directly discharged.
The deamination membrane unit comprises a pH adjusting tank, a deamination membrane device and a buffer tank. The pH equalizing basin is intake the side and is connected with evaporimeter comdenstion water outlet, and the comdenstion water after pH value adjusts passes through pipeline access deamination membrane device, and deamination membrane shell process product water drains into the buffer pool, carries out acid-base neutralization in the buffer pool, and direct discharge to reach standard after the pH callback, the tube side adopts sulphuric acid as the absorption liquid, permeates the ammonia of film component in the feed liquid in the absorption shell side, and ammonium sulfate purity can reach more than 98% after evaporation crystallization alone, can carry out recovery processing as the ammonium salt.
The foregoing embodiments and description in the specification should be considered as the implementation principle and further explanation and guidance of the present invention, and not in a limiting sense, and not limited to the examples provided above. It will be apparent to those skilled in the art that various modifications, substitutions and variations can be made in the embodiments without departing from the spirit and scope of the utility model.
Claims (9)
1. A landfill leachate treatment system is characterized by comprising a pretreatment unit, a coagulation reaction tank, a sedimentation tank, a raw water concentration tank, a microfiltration membrane unit, an evaporation unit, a micro-interface wet oxidation unit and a deamination membrane unit;
the pretreatment unit, the coagulation reaction tank, the sedimentation tank, the raw water concentration tank and the microfiltration membrane unit are sequentially connected;
the pretreatment unit adopts a full-automatic back-flushing filter and is used for removing particles, colloids and suspended matters contained in the percolate; a water outlet of a filter of the pretreatment unit is connected with a coagulation reaction tank;
the coagulation reaction tank comprises two reaction water tanks with communicated bottoms, reaction tank overflow ports are uniformly formed in the upper parts of the two reaction tanks, and the coagulation reaction tank is communicated with the sedimentation tank through the reaction tank overflow ports;
the sedimentation tank is used for settling coagulated particles, and supernatant is obtained after the coagulated particles are settled; the upper part of the sedimentation tank is provided with a sedimentation tank overflow port, and supernatant flows into the raw water concentration tank through the sedimentation tank overflow port;
the raw water concentration tank is connected with the microfiltration membrane unit, water circulation is carried out between the raw water concentration tank and the microfiltration membrane unit, and meanwhile, clear water filtered by the microfiltration membrane unit enters the evaporation unit;
the concentrated solution discharge port of the evaporation unit is connected with the micro-interface wet oxidation unit through a high-pressure pump, the micro-interface wet oxidation unit is used for oxidizing the concentrated solution and then returning to the evaporation unit, and the condensed water outlet end of the evaporation unit is connected with the deamination membrane unit.
2. The landfill leachate treatment system of claim 1, wherein the microfiltration membrane unit comprises a microfiltration membrane device, a concentrate tank and an intermediate tank, wherein two concentrate pipelines are arranged on the concentrate side of the microfiltration membrane device, one of the concentrate pipelines is connected with the raw water concentrate tank, the other of the concentrate pipelines is connected with the concentrate tank, concentrate circulation is continuously performed between the raw water concentrate tank and the microfiltration membrane device, part of the concentrate is collected by the microfiltration membrane device and enters the concentrate tank, the clear water side of the microfiltration membrane device is connected with the intermediate tank, and the intermediate tank is a microfiltration membrane produced water collection tank.
3. The landfill leachate treatment system of claim 2, wherein the microfiltration membrane device employs a tubular microfiltration membrane.
4. The landfill leachate treatment system of claim 1, wherein the micro-interface wet oxidation unit comprises a preheater, a micro-interface wet oxidation reactor, a heat exchanger and a gas-liquid separator, the concentrated solution discharged from the concentrated solution discharge port of the evaporation unit passes through the preheater and then reaches the micro-interface wet oxidation reactor, the micro-interface wet oxidation reactor uses high-pressure air or oxygen as an oxidant to perform oxidation treatment on the concentrated solution, the oxidized concentrated solution enters the gas-liquid separator, and the liquid outlet end of the gas-liquid separator is connected with the evaporation unit after part of heat is recovered by the heat exchanger.
5. The landfill leachate treatment system of claim 1, wherein the deamination membrane unit comprises a pH adjusting tank, a deamination membrane device and a buffer tank;
the evaporation unit comdenstion water outlet end is connected the side of intaking of pH equalizing basin, and the comdenstion water after pH value adjusts passes through the pipeline and inserts the deamination membrane device, and deamination membrane device shell process product water drains into the buffer pool, carries out the acid-base neutralization in the buffer pool, and the tube side adopts sulphuric acid as the absorption liquid, permeates the ammonia of membrane element in the feed liquid in the absorption shell process.
6. The landfill leachate treatment system of claim 1, wherein the evaporation unit comprises an evaporation device and a tail gas treatment device, and the non-condensable gas outlet of the evaporation device is connected with the tail gas treatment device.
7. The landfill leachate treatment system of claim 1, wherein a stirring device is disposed in each of the two reaction pools of the coagulation reaction pool.
8. The landfill leachate treatment system of claim 2, further comprising a sludge pressure filtration device; the bottom parts of the sedimentation tank, the raw water concentration tank and the concentrated water tank of the microfiltration membrane unit are all provided with pipelines connected to a sludge filter pressing device for discharging sludge, and the sludge filter pressing device returns liquid to the sedimentation tank after filtering the sludge.
9. The landfill leachate treatment system of claim 2, wherein the intermediate tank of the microfiltration membrane unit is provided with a pH detection device and an acid addition port for controlling the pH of the feed solution entering the evaporation tank.
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| CN202122257482.7U CN216236502U (en) | 2021-09-17 | 2021-09-17 | Landfill leachate treatment system |
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| CN202122257482.7U CN216236502U (en) | 2021-09-17 | 2021-09-17 | Landfill leachate treatment system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114956432A (en) * | 2022-06-27 | 2022-08-30 | 中节能工程技术研究院有限公司 | Waste alkali liquor recycling method and system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114956432A (en) * | 2022-06-27 | 2022-08-30 | 中节能工程技术研究院有限公司 | Waste alkali liquor recycling method and system |
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Effective date of registration: 20231220 Address after: No.57, Qiande Road, Jiangning District, Nanjing, Jiangsu, 211100 Patentee after: NANJING WONDUX ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Patentee after: Inner Mongolia Yanqing Environmental Technology Co.,Ltd. Address before: 211122 No. 57, Qiande Road, Jiangning District, Nanjing City, Jiangsu Province Patentee before: NANJING WONDUX ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. |
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